US1872011A - Improved process for treating hydrocarbons - Google Patents
Improved process for treating hydrocarbons Download PDFInfo
- Publication number
- US1872011A US1872011A US289705A US28970528A US1872011A US 1872011 A US1872011 A US 1872011A US 289705 A US289705 A US 289705A US 28970528 A US28970528 A US 28970528A US 1872011 A US1872011 A US 1872011A
- Authority
- US
- United States
- Prior art keywords
- gas
- oil
- hydrogen
- pressure
- improved process
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 229930195733 hydrocarbon Natural products 0.000 title description 12
- 150000002430 hydrocarbons Chemical class 0.000 title description 12
- 238000000034 method Methods 0.000 title description 10
- 239000003921 oil Substances 0.000 description 20
- 239000007789 gas Substances 0.000 description 17
- 239000001257 hydrogen Substances 0.000 description 11
- 229910052739 hydrogen Inorganic materials 0.000 description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000003575 carbonaceous material Substances 0.000 description 3
- 230000029087 digestion Effects 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000005201 scrubbing Methods 0.000 description 3
- 230000001066 destructive effect Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 241001122767 Theaceae Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- UOUJSJZBMCDAEU-UHFFFAOYSA-N chromium(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Cr+3].[Cr+3] UOUJSJZBMCDAEU-UHFFFAOYSA-N 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical compound [O-2].[Fe+2] VBMVTYDPPZVILR-UHFFFAOYSA-N 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000011299 tars and pitches Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
Definitions
- the present invention relates to the art of obtaining valuable low' boiling distillates from carbonaceous material and more specifically comprises an improved method for decomposing carbonaceous materials in the presence of hydrogen.
- My invention will be understood from the following description and the drawing which illustrates one form of apparatus suitable for use with my method.
- the drawing is a semi-diagrammatic view in sectional elevation of an apparatus constructed according to my invention and showin the flow of materials.
- reference numeral 1 denotes a pipe coil arranged in a furnace setting 2.
- the materiaLheated bypassage through coil 1 is discharged through line 3,.which may be fitted with a check valve 4, into a digestionchamber'5.
- the digestion chamber may be of any preferred design but it should be adapted to withstand pressure in excess of 200 atmospheres and it is protected against loss of heat. It is advantageous to construct the drum with a relatively thin inner wall 5a, and insulating layer -6 and a relatively heavy wall 5b to withstand the pressure.
- the contents of the digestion chamber is kept in thorough agitation by a stirring means '7 or by any other suitable means, and temperature is maintained betweenpreferable limits of 750 and 970 F.
- the fresh oil charged with dissolved gas is passed by line 28 and pump 29 to heat exchanger 17 and from thence by line 30 which maybe fitted with a reduction valve R to a preliminary still or separator 31.
- the dissolved gases are removed and conducted to storage (not shown) for use as fuel or otherwise, while the liquid is pumped by pump 32 through line 33 to coil 1.
- oils such as crude or reduced crude, or any out therefrom heavler than gasoline, may be treated so alone or may be admlxed with tars and pitches or solid bitumens or powdered coil.
- - Decompogition takes place under the action of high pressure of hydrogen to yield substantial quantities of low boilin
- Thefluidmass is heated y passage through coil 1 tea, decomposing temperature, preferably between 750 and 970 F. and I prefer to provide hydrogen in contact with the oil during such heating.
- Catalysts may also be 90 hydrocarbon oils.
- the heated mass is discharged into the drum 5 which is maintained at a temperature of between 750 and 970 F., prefer ably by recirculation of oil,has been described.
- Hydrogen is also circulated through the oil. It will be understood that hydrogen is consumed in the reaction which takes place and that a large excess over that which actually enters into combination is circulated through the apparatus. Pressure during the heating and digestion stages is in excess of 50 atmospheres and preferably from 100 to 200 atmospheres although higher pressures may be used.
- the hydrocarbon gas dissolved together with hydrogen sulfid is removed from the oil by preferably heating alone or by heating together with a reduction of pressure. Although only a simple separator is shown, a stripping column with bell cap plates or the equivalent may be substituted.
- My invention is not to be limited to the specific form of apparatus used to illustrate my process ,but. may be used in connection with any continuous form of apparatus for simultaneous decomposition and hydrogenation of carbonaceous materials.
- My invention is not to be limited by any theory of the process nor by any specific example given merely by way of illustration but only by the following claims in which I wish to claim all novelty inherent in the invention.
Description
Aug. 16, 1932.-
1 R. P. RUSSELL IMPROVED PROCESS FOR TREATING HYDROCARBONS Fi1ed July 2, 1928 III .llllld H I IIL ll Ill- ROBERTPRUS-SELL avwewcoz Patented Aug. 16, 1932 UNHTED STATES PATENT OFFICE ROBERT P. RUSSELL, F BATON ROUGE, LOUISIANA, ASSIGNOR 1'0 STANDARD-1:..G.
- COMPANY IMPROVED PROCESS E01 TBEATING HYDROCARBONS Application. filed July 2,
The present invention relates to the art of obtaining valuable low' boiling distillates from carbonaceous material and more specifically comprises an improved method for decomposing carbonaceous materials in the presence of hydrogen. My inventionwill be understood from the following description and the drawing which illustrates one form of apparatus suitable for use with my method.
The drawing is a semi-diagrammatic view in sectional elevation of an apparatus constructed according to my invention and showin the flow of materials.
eferring to the drawing, reference numeral 1 denotes a pipe coil arranged in a furnace setting 2. The materiaLheated bypassage through coil 1 is discharged through line 3,.which may be fitted with a check valve 4, into a digestionchamber'5. The digestion chamber may be of any preferred design but it should be adapted to withstand pressure in excess of 200 atmospheres and it is protected against loss of heat. It is advantageous to construct the drum with a relatively thin inner wall 5a, and insulating layer -6 and a relatively heavy wall 5b to withstand the pressure. The contents of the digestion chamber is kept in thorough agitation by a stirring means '7 or by any other suitable means, and temperature is maintained betweenpreferable limits of 750 and 970 F. either-by internal heaters (not shown) or, as I prefer, by circulating a part of the oil from drum 5 through line 8, pump 9 and line 10, back to coil land drum 5. 1 4 HydrogenQ-or a gas containing a substantial quantity of hydrogen, is sprayed into drum 5 by spray pipe 11 which is fed from a supply line 13 and a further quantity of such gas may be added to the oil returning to coil 1. The gas is preferably added in a finely divided state by passing through a. porous plate or by passage with the oil through any convenient type of mixer, shown generally at 1 1. Vapor from drum 5 is conducted .by pipe 1928. Serial No. 289,705.
15 to a pair of heat exchangers 16 and 17 arranged in series for the passage of the vapor.
- Readily liquefied products are condensed and the mixture of condensate and gas is discharged into a separator 18 from which liquid is withdrawn to storage (not shown) by line 18a and through cooler 18?). Vapor passes by line 19 to a scrubbing tower 20 which is fed at the top with fresh oil to be fed to coil 1 and drum 5, as will be described. The
through exchanger 16 for preheating by lines 25 and 26 before entering line 13, as will be understood. Make up hydrogen is added by pipe 27.
The fresh oil charged with dissolved gas is passed by line 28 and pump 29 to heat exchanger 17 and from thence by line 30 which maybe fitted with a reduction valve R to a preliminary still or separator 31. The dissolved gases are removed and conducted to storage (not shown) for use as fuel or otherwise, while the liquid is pumped by pump 32 through line 33 to coil 1.,
In the operation of my process, oils such as crude or reduced crude, or any out therefrom heavler than gasoline, may be treated so alone or may be admlxed with tars and pitches or solid bitumens or powdered coil.- Decompogition takes place under the action of high pressure of hydrogen to yield substantial quantities of low boilin Thefluidmass is heated y passage through coil 1 tea, decomposing temperature, preferably between 750 and 970 F. and I prefer to provide hydrogen in contact with the oil during such heating. Catalysts may also be 90 hydrocarbon oils.
present suspended in the oil, such as finely ground iron oxid or molybdenum oxid or materials.
chromium oxid or a mixture of any of these The heated mass is discharged into the drum 5 which is maintained at a temperature of between 750 and 970 F., prefer ably by recirculation of oil,has been described. Hydrogen is also circulated through the oil. It will be understood that hydrogen is consumed in the reaction which takes place and that a large excess over that which actually enters into combination is circulated through the apparatus. Pressure during the heating and digestion stages is in excess of 50 atmospheres and preferably from 100 to 200 atmospheres although higher pressures may be used.
Normally liquid hydrocarbons are condensed from the vapors and removed to storage, while uncondensed gases are scrubbed with fresh oil under high pressure, and preferably at temperatures under 100 F. so that a portion of the hydrocarbons present in the gas mixture is dissolved in the oil. It is not necessary to dissolve the entire hydrocarbon content of the gas but it is desired to prevent the recirculated gas from building up to over about 35% hydrocarbon and preferable to maintain the percentage of hydrogen above 50%. Pressure prevailing in absorption tower 20 is in excess of 50 atmospheres and is preferably 100 or 200 atmospheres, substantially equal to the full pressure of the retort 5.
The hydrocarbon gas dissolved together with hydrogen sulfid is removed from the oil by preferably heating alone or by heating together with a reduction of pressure. Although only a simple separator is shown, a stripping column with bell cap plates or the equivalent may be substituted.
My invention is not to be limited to the specific form of apparatus used to illustrate my process ,but. may be used in connection with any continuous form of apparatus for simultaneous decomposition and hydrogenation of carbonaceous materials. My invention is not to be limited by any theory of the process nor by any specific example given merely by way of illustration but only by the following claims in which I wish to claim all novelty inherent in the invention.
I claim: I
1. In a process for the destructive hydrogenation of hydrocarbon oils in which the oil is treated in a reaction zone with a gas rich in free hydrogen under pressure in excess of 50 atmospheres and at temperature of the order of 750 to 970 F., the improved steps of separating the reaction gas from the liquid product, scrubbing the gas with the feed oil underpressure and attemperature below about 100 F. whereby a large portion of the hydrocarbon constituents of the gas are dissolved and a gas richerin hydrogen is obtained, heating and reducing pressure on the feed oil whereby the dissolved gas rich in hydrocarbons is expelled and discarded, and then forcing the oil and the undissolved gas rich in hydrogen into the reaction zone.
2. Process according to claim 1 in which the destructive hydrogenation is carried out at a pressure of the order of 200 atmospheres, the feed oil is heated by indirect contact with the hot products from the reaction zone and the gas-scrubbing step is accomplished under substantially the same pressure as prevails in the reaction chamber.
ROBERT P. RUSSELL.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US289705A US1872011A (en) | 1928-07-02 | 1928-07-02 | Improved process for treating hydrocarbons |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US289705A US1872011A (en) | 1928-07-02 | 1928-07-02 | Improved process for treating hydrocarbons |
Publications (1)
Publication Number | Publication Date |
---|---|
US1872011A true US1872011A (en) | 1932-08-16 |
Family
ID=23112724
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US289705A Expired - Lifetime US1872011A (en) | 1928-07-02 | 1928-07-02 | Improved process for treating hydrocarbons |
Country Status (1)
Country | Link |
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US (1) | US1872011A (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2429115A (en) * | 1944-04-03 | 1947-10-14 | Standard Oil Dev Co | Hydrogenation process and apparatus |
US2982360A (en) * | 1956-10-12 | 1961-05-02 | Int Nickel Co | Protection of steel oil and/or gas well tubing |
US3193595A (en) * | 1962-01-31 | 1965-07-06 | Standard Oil Co | Hydrocarbon conversion |
US3346485A (en) * | 1964-10-01 | 1967-10-10 | Exxon Research Engineering Co | Prevention of deterioration of ferrous containers by molecular sieve displacing agent |
-
1928
- 1928-07-02 US US289705A patent/US1872011A/en not_active Expired - Lifetime
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2429115A (en) * | 1944-04-03 | 1947-10-14 | Standard Oil Dev Co | Hydrogenation process and apparatus |
US2982360A (en) * | 1956-10-12 | 1961-05-02 | Int Nickel Co | Protection of steel oil and/or gas well tubing |
US3193595A (en) * | 1962-01-31 | 1965-07-06 | Standard Oil Co | Hydrocarbon conversion |
US3346485A (en) * | 1964-10-01 | 1967-10-10 | Exxon Research Engineering Co | Prevention of deterioration of ferrous containers by molecular sieve displacing agent |
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